CN1919403A - Method and apparatus for separating oil and water - Google Patents
Method and apparatus for separating oil and water Download PDFInfo
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- CN1919403A CN1919403A CN 200610110057 CN200610110057A CN1919403A CN 1919403 A CN1919403 A CN 1919403A CN 200610110057 CN200610110057 CN 200610110057 CN 200610110057 A CN200610110057 A CN 200610110057A CN 1919403 A CN1919403 A CN 1919403A
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Abstract
In the oil and water separating method and the oil and water separating apparatus, in particular relating to providing tiny bubbles to the treated liquid of a treating tank, which are for floating the oil component contained in a liquid to be treated together with bubbles to separate oil and water by supplying the bubbles into the liquid to be treated stored in a treating tank; air is mixed with the liquid to be treated taken out from the lower part of the treating tank 11, the pressure of the liquid is raised by a circulation pump 31 to be jetted from a nozzle 33 provided at the lower part of the treating tank 11 to return and circulate the liquid to be treated to the treating tank 11, and an untreated liquid to be treated is supplied to a circulation pipeline of the liquid to be treated or to the lower part of the treating tank 11. A small amount of a calcium chloride, a hydrochloric acid and a sodium hydroxide are added to this line to promote agglomeration of the oil in order to improve the oil separating performance. According to this invention, it can make it possible to separate a water containing a low hydrophobic oil at a high speed into oil and water up to the effluent standard.
Description
Technical field
The present invention relates to oil-water separation method and oily-water seperating equipment, be particularly related to use and supply with small bubble to the processed liquid of treatment trough, the oil content that is included in the processed liquid is floated with bubble, utilize the oil-water separation method and the oily-water seperating equipment that processed liquid are separated into the come-up separation method of water and oil content.
Background technology
As the separator that uses the come-up separation method, there is patent documentation described as follows 1 described, fluid intake at turbulence pump is provided with gas suction device, in process, make air dissolves (gas-liquid mixed dissolving) in processed liquid with the turbulence pump pressurization, by in treatment trough, spraying decompression, make and produce small bubble in the processed liquid in the treatment trough by nozzle.
[patent documentation 1] spy opens the 2003-236305 communique
Summary of the invention
In above-mentioned prior art, when the hydrophobicity of oil own was high, the small bubble that produces in the treatment trough combined with oil content, and oil content and bubble float together, can water-oil separating.But when the hydrophobicity of oil itself was low, the combination of oil content and small bubble was not fully carried out, can not water-oil separating.
For example, contain the water (draining) of the lubricated wet goods mineral oil that produces by reciprocating compressor and screw compressor etc., often can not separating oil to the draining benchmark 5mg/L of mineral oil.
So, the object of the present invention is to provide a kind ofly can make the water high speed water-oil separating that contains the low oil of hydrophobicity, until oil-water separation method that reaches the draining benchmark and oily-water seperating equipment.
In order to achieve the above object, oil-water separation method of the present invention is characterised in that, supply with small bubble at processed liquid to treatment trough, the oil content and the bubble that are included in the processed liquid are floated together, make in the oil-water separation method of processed liquid water-oil separating, supply with bubble to processed liquid, described processed liquid has been supplied with at least a, calcium chloride in hydrochloric acid, sulfuric acid and the nitric acid and at least a and NaOH in the magnesium chloride.
In order to achieve the above object, oil-water separation method of the present invention is characterised in that, supply with small bubble at processed liquid to treatment trough, the oil content and the bubble that are included in the processed liquid are floated together, make in the oil-water separation method of processed liquid water-oil separating, after at least a at least a and calcium chloride and the magnesium chloride supplied with to processed liquid in hydrochloric acid, sulfuric acid and the nitric acid, supply with NaOH, supply with bubble thereafter.
In order to achieve the above object, oily-water seperating equipment of the present invention is characterised in that, supply with small bubble at processed liquid to treatment trough, the oil content and the bubble that are included in the processed liquid are floated together, make in the oily-water seperating equipment of processed liquid water-oil separating to comprise: with pump from this treatment trough the processed liquid of sucking-off, pressurization, from the 1st pipe arrangement system that the external circulating system of the nozzle ejection that is located at this treatment trough bottom constitutes; Suction is located at the 2nd pipe arrangement system of air of the suction side of this pump; The 3rd at least a pipe arrangement of supplying with in hydrochloric acid, sulfuric acid and the nitric acid to the processed liquid of this treatment trough is; Supply with at least a the 4th pipe arrangement system in calcium chloride water and the magnesium chloride brine; Supply with the 5th pipe arrangement system of sodium hydrate aqueous solution.
And then, be provided with the control device that carries out carrying out following operation: make this pump running, this external circulating system is played a role; Supply with at least a, calcium chloride water in hydrochloric acid, sulfuric acid and nitric acid and at least a and sodium hydrate aqueous solution in the magnesium chloride brine by the 3rd～the 5th each pipe arrangement system; System sucks air by the 2nd pipe arrangement, pressurizes in this pump, makes air dissolves in this processed liquid, is sprayed by this nozzle together as bubble and processed liquid.
This control device is made of the 1st control device and the 2nd control device.The 2nd control device makes this pump running, and external circulating system is played a role.After the 2nd control device is supplied with at least a and sodium hydrate aqueous solution at least a, calcium chloride water in hydrochloric acid, sulfuric acid and nitric acid and the magnesium chloride brine by each pipe arrangement system of the 3rd～the 5th, system sucks air by the 2nd pipe arrangement, in this pump, pressurize, make air dissolves in this processed liquid, spray by this nozzle together as bubble and processed liquid.
According to the present invention, the surfactant in the processed liquid is because hydrochloric acid, sulfuric acid and nitric acid isoreactivity are lowered, and oil content is by calcium chloride (CaCl
2) and magnesium chloride (MgCl
2) cohesion, NaOH (NaOH) promotes this cohesion, the small oil content of dispersion becomes the result of combination and then enlarged diameter, and not only floats easily, and also easy and micro-bubble absorption, the easier come-up that becomes, water-oil separating is carried out at a high speed.
According to the present invention, by reducing the addition that metal is had corrosive hydrochloric acid, sulfuric acid and nitric acid etc. and calcium chloride, magnesium chloride etc., improve the concentration of sodium hydrate aqueous solution, keep the oil content flocculating result as a whole, make the pH value of handling back liquid simultaneously in bringing up to the draining benchmark, the corrosivity of hydrochloric acid, sulfuric acid and nitric acid etc. and calcium chloride, magnesium chloride etc. is reduced, and all metal parts such as treatment trough and pipe arrangement are difficult to corrosion.
Acid descends the activity of surfactant, though water-oil separating is easy, hinders the absorption of isolated oil content and bubble.Therefore, with hydrochloric acid, sulfuric acid and nitric acid etc. profit is separated easily, make with calcium chloride, magnesium chloride etc. on the basis of oil content cohesion, by processed liquid is made alkalize, it is easy to form the absorption that makes with bubble, the quantity delivered and the raising that reduce acid and flocculating agent separate the come-up function, reach water-oil separating at a high speed.
Because the main component of the bittern of using when calcium chloride, magnesium chloride etc. are manufacturing bean curd, it is the product that is used for food, owing to be, use in the NaOH and draining on the basis of hydrochloric acid, sulfuric acid and nitric acid etc., so do not pollute the environment with processed their aqueous solution of liquid dilution.
Thereby, even contain the water of the low oil of hydrophobicity, also can carry out water-oil separating at a high speed, conform with the draining benchmark until reaching, oil content reclaims, and the water former state is discarded.
Description of drawings
Fig. 1 is the figure that expression becomes the oily-water seperating equipment of an embodiment of the present invention;
Fig. 2 is the figure that expression becomes the oily-water seperating equipment of another embodiment of the present invention;
Fig. 3 is the figure that expression becomes the oily-water seperating equipment of the another embodiment of the present invention;
Fig. 4 is that expression becomes the present invention figure of the oily-water seperating equipment of an embodiment again;
Fig. 5 is the figure that expression becomes the oily-water seperating equipment of other embodiment of the present invention;
Fig. 6 is the figure that expression becomes the oily-water seperating equipment of another other embodiment of the present invention;
Fig. 7 is the figure that expression becomes the oily-water seperating equipment of another other embodiment of the present invention;
Fig. 8 is the figure of one of expression oil-water separation of the present invention example.
The specific embodiment
Below, the oil-water separation method and the oily-water seperating equipment of embodiment of the present invention are described with reference to the accompanying drawings.In whole figure,, same object is used identical quotation mark for fear of the repetition of explanation.
The oily-water seperating equipment that becomes an embodiment of the present invention 10 shown in Figure 1 uses the draining of being discharged by air compressor as an example as handled thing.
In Fig. 1, in treatment trough 11, have in groove, store processed liquid carry out water-oil separating separation portion (in claims, being designated as treatment trough) 81, be recovered in this separation portion 81 come-up, the last oil slick acceptance division 83 of the oil content that separates, be provided with two ones 81 of separation, 83 shield 12.In the lower sidewall of treatment trough 11, in separation portion 81, be connected with air pocket separation portion 13.
Be installed in pipe arrangement 30 at the end of the separation portion 81 in the treatment trough 11 by valve (switch valve, all the same in following all valves) 36, be connected with circulating pump 31 by pipe arrangement 32, the outlet of circulating pump 31 (discharge) side line 37 be arranged on air pocket and separate the interior nozzle 33 of portion 13 and be connected.When pipe arrangement 30,32,37 is formed in circulating pump 31 runnings, by the processed liquid in the pipe arrangement 30 sucking-off separation portions 81, by the external circulating system (the 1st pipe arrangement system) of nozzle 33 ejections that are located at treatment trough 81 bottoms.
In pipe arrangement 32, connect an end of air supply pipe 41 with valve 42, the other end of air supply pipe 41 is to atmosphere opening, and air supply pipe 41 constitutes the 2nd pipe arrangement system of the air that sucks the suction side that is located at circulating pump 31.Be connected with treatment trough 11 from the pipe arrangement 38 of outlet side pipe arrangement 37 branches of circulating pump 31, have valve 39, pipe arrangement 38 to be formed in bypass tubing in the external circulating system in the centre.
As described later,, attract air, pressurize, make it to be dissolved in the processed liquid simultaneously, be dissolved with the processed liquid of air from nozzle 33 ejections by air supply pipe 41 by the running of circulating pump 31.Pipe arrangement 38 constitutes the external circulating system that separates the processed liquid in the portion 81 with pipe arrangement 30,32,37.At circulating pump in the specified time limit of 31 durations of runs, with low pressure from the front end of pipe arrangement 38 to the processed liquid of treatment trough 41 ejections.
As an example of circulating pump 31, use turbulence pump, though not shown, be provided with the table of measuring processed hydraulic coupling (hydraulic pressure) at the outlet side of circulating pump 31.
Also can in pipe arrangement 32, connect the supply pipe 23 that has supply pump 21 and valve 22, constitutes the feed system of untreated processed liquid.Supply pipe 23 is connected with the bottom of separating portion 81, also can supply with untreated processed liquid to separation portion 81.
In the pipe arrangement 32 of the suction side of circulating pump 31, connect by valve 77 from the supply port of the pipe arrangement 72 of NaOH (NaOH) aqueous solution case 71, pipe arrangement 72 constitutes the 5th pipe arrangement system.And in pipe arrangement 32, from calcium chloride (CaCl
2) supply port of pipe arrangement 92 of aqueous solution case 91 connects by valve 97, pipe arrangement 92 constitutes the 4th pipe arrangement system.And then, in pipe arrangement 32, connecting by valve 107 from the supply port of the pipe arrangement 102 of hydrochloric acid (HCl) case 101, pipe arrangement 102 constitutes the 3rd pipe arrangement system.
Be provided with the discharge pipe 51 of the processed liquid after discharge handling on the top of separation portion, discharge pipe 51 be from the connecting portion that separates portion 81 (base) promote, make its downstream be positioned at than with the pipe arrangement of the lower position of the connecting portion that separates portion 81, valve 52 is arranged therebetween.The highest order of discharge pipe 51 is lower than the highest order of the shield 12 of treatment trough 11, and holding position difference D1.
Therefore, when supplying with processed liquid and make it to store in separation portion 81, as long as relief valve 52, processed liquid just flows out from discharge pipe 51, and the processed liquid level 61 in the separation portion 81 is limited by the highest order of discharge pipe 51.If shut off valve 52 is supplied with processed liquid in separating tank 81, owing to the highest order of processed liquid level 61 than discharge pipe 51 also rises, discharge pipe 51 has the function of discharging processed liquid, adjustment water level by open and close valve 52.
Be located at pipe arrangement 53 on the discharge pipe 51 to atmosphere opening so that be unlikely to because of the siphon effect draining to the highest level face of discharge pipe 51.On the top of processed liquid level 61, form the come-up oil level 62 of the last oil slick that rises by water-oil separating.
Be provided with the dividing plate 15 micro-bubble in preventing from separation portion 81 to rise and the elaioleucite processed liquid from the processing of outflow is sneaked into by separation portion 81 by discharge pipe 51 after, shape pouch suction portion 82.Promptly by making by the discharge of the processed liquid in the discharge pipe 51 and slower than the rate of climb of bubble by the decrease speed of the processed liquid in the suction portion 82 of the inlet area decision of suction portion 82, micro-bubble in rising separation portion 81 in and elaioleucite can not flow into suction portion 82 and from discharge pipe 51 outflows.
The highest order of dividing plate 15 is than the highest order of discharge pipe 51, and promptly the processed liquid level 61 during relief valve 52 is low, is keeping alternate position spike D2.Make the highest order ratio of dividing plate 15 and connecting portion (base) height of the portion that separates 81 of discharge pipe 51, keeping alternate position spike D3.
The bottom of oil slick portion 83 on receiving is provided with discharge and crosses the oil content discharge pipe 55 that shield 12 flows into the waste oil 63 of (overflow) from separation portion 81.In addition, show among the figure, be provided with pipe arrangement to the outside, be provided with valve therebetween, when being necessary to discharge the liquid of separation portion 81 inside, use them from the bottom of treatment trough 11.
In separation portion 81, be provided with temperature measuring device 84, can measure the temperature of the processed liquid in the separation portion 81.Also can replace temperature measuring device 84,, measure the temperature of processed liquid to the pipe arrangement 37 of nozzle 33, temperature measuring device being set through circulating pump 31 from pipe arrangement 30.
Secondly, the running of oily-water seperating equipment shown in Figure 1 is described.
From the draining (summer) when absolute humidity is high that air compressor is discharged, drain discharge is many, and the concentration of oil in the draining is low.And when absolute humidity is low (winter or spring and autumn), drain discharge is few, the concentration of oil height in the draining.
At this, the draining when at first absolute humidity being hanged down is handled running and is described.
As preparation, make valve 52 be in the state of closing, in separation portion 81, be full of clear water or handle after the state of processed liquid under, make circulating pump 31 runnings, valve 22 cuts out, and valve 36,42 is open, dissolving flows into from air dispensing pipe 41 with air.The power of circulating pump 31 becomes heat and passes to processed liquid, the temperature of the processed liquid in the separation portion 81 is risen, so the density of processed liquid diminishes.In addition, for the density that makes processed liquid diminishes, also can in separation portion 81, dispose the heater that the temperature that is used to make processed liquid rises.
After processed liquid rises to predetermined temperature, stop the running of the circulating pump 31 in the circulatory system, shut off valve 42 makes 22 one-tenth open states of valve of processed liquid supply system, and running supply pump 21 is supplied with the processed liquid of the state that is untreated.Processed liquid flows into separation portion 81 through the path and the pipe arrangement 32,37 of pipe arrangement 30 from nozzle 33.
Processed liquid be since score from portion 81 in clear water or the processing after processed liquid temp low, density is big, accumulates in the bottom of separation portion 81; The low processed liquid of concentration of oil after the little processing of density is pulled to the form on the top of separation portion 81, discharges through discharge pipe 51 and valve 52 from suction portion 82.For example, if the volume from dividing plate 15 upper ends to the bottom of separation portion 81 is 40L, processed liquid temp after clear water or the processing is 320K, the temperature of processed liquid of state of being untreated is 283K, with the be untreated supply of processed liquid of state of 20L/h, the processed liquid after only handling just can be discharged more than the 30L.As an example, as clear water or the processed liquid of the processed liquid after handling and the state that the is untreated 20L that all respectively does for oneself, the supply processed liquid of state that is untreated to separation portion 81 in.
If the processed liquid of only discharging after handling finishes, make 52 one-tenth closed conditions of valve 22 and valve, supply pump 21 is stopped, the supply of the processed liquid of the state that is untreated is ended, and makes 39 one-tenth open states of valve, implements the groove outer circulation of being undertaken by circulating pump 31 (the 1st control).At this moment, because the processed liquid that also flowing in pipe arrangement 38, by the existence of nozzle 33, the outlet pressure of high circulating pump 31 descends, and according to the discharge characteristic of circulating pump 31, circular flow significantly increases.Then, control valve 36 confirms that with the not shown pressure gauge that goes out pump entry pressure ratio atmosphere forces down, relief valve 97, with the pressure differential of this pressure and calcium chloride water 91 as driving force, by the calcium chloride water of case 91 supply required amounts, shut off valve 97.Equally, relief valve 107, by the hydrochloric acid of case 101 supply required amounts, afterwards, shut off valve 107.Equally, relief valve 77, by the sodium hydrate aqueous solution of case 71 supply required amounts, afterwards, shut off valve 77.
By these operations, processed liquid and interpolation medicine fully mix, and reduce surfactant activity with hydrochloric acid, the oil of colloidal substance dispersion as a result becomes and condenses easily, and making elaioleucite cohesion, sodium hydrate aqueous solution promote its cohesion with calcium chloride water, it is big that the particle of the elaioleucite of cohesion directly becomes.The open circular flow that improves of valve 39 fully mixes processed liquid and interpolation medicine.
Then, if shut off valve 39 makes 42 one-tenth open states of valve, dissolving flows into from air supplying tubing 41 with air.By pressurizeing with circulating pump 31, being dissolved in air capacity in the processed liquid becomes under pressurized state and defers to Henry (Henry) rule, pressure relevant with the processed liquid after clear water that flows in pipe arrangement 37 or the processing and the flow that flows through in pipe arrangement 37 are proportional, and the air quantitative change of dissolving is many.In addition, the temperature of the processed liquid after clear water that flows in pipe arrangement 37 or the processing is low more, and the air capacity of dissolving is many more.Setting pressure, flow are the certain value running in real-world operation.
By this running (the 2nd control), to separating portion 81 in, spray draining by nozzle 33 with micro-bubble, the oil content that condenses with the calcium chloride water in the draining is attached to floating on the micro-bubble, and oil content separates from processed liquid (water).Sodium hydrate aqueous solution makes the oil content of cohesion attached to carrying out easily on the micro-bubble.
The power of circulating pump 31 becomes heat and passes to processed liquid, and fluid temperature rises, and the air capacity of dissolving reduces.Therefore, obtain the relation of fluid temperature and dissolved air amount in advance,, regulate, make from the dissolving of air supply pipe 41 inflows roughly consistent with the amount of bubble floating treatment trough 11 with air capacity with valve 42 according to the fluid temperature of obtaining with temperature measuring device 84.
The air pocket of the bubble that diameter is big is because buoyancy is big, also fast than the micro-bubble come-up, come-up is helpless to water-oil separating rapidly, make the movement disorder in separation portion 81, the obstruction micro air bubble contacts with oil content, though separating property is descended, but prevent because such surplus air causes the continuous generation of air pocket, when producing air pocket, make it to be sorted in the discharge pipe 14 of air pocket separation portion 13, may be from the air pocket of nozzle 33 ejection not round separation portion 81, the water-oil separating performance can not descend.
By shut off valve 52, micro-bubble is present in the processed liquid of separation portion 81, and processed liquid level 61 is also higher than the extreme higher position of discharge pipe 51.Under this state, at processed liquid level 61 upsides of separation portion 81 inside, the oil of come-up accumulates, and the upper end position that makes shield 12 is than floating oil level 62 height of going up, and in the circulation of processed liquid, last oil slick can not overflow from the shield 12 oil slick acceptance division 83 that makes progress.
Oil content utilizes micro-bubble to rise from the bottom of separation portion 81 in the groove outer circulation, can carry out water-oil separating at a high speed.According to the inventor's etc. observation, confirm preceding half 50% time in the groove outer circulation, the concentration of oil of the processed liquid of the state that is untreated drop to intermediate concentration following about 1/5th; In later half 50% time, further drop to about 1/5th low concentration (aimed concn) of its concentration from the concentration of oil below the middle concentration.Half ratio that reduces is identical degree in front and back, but sees by absolute value, will be separated at preceding medium-sized half oil content.
Processed liquid in the separation portion 81 is as if the concentration of oil that has reduced as target, and circulating pump 31 stops, and valve 42 cuts out, and valve 22 and valve 52 are opened, and makes supply pump 21 runnings, supplies with the processed liquid of the state that is untreated from the bottom of separation portion 81.During this period, the processed liquid same amount of processed liquid after the processing on separation portion 81 tops and the new state of supplying with that is untreated just flows out from discharge pipe 51.
The more than running of the supply pump 21 of Shuo Ming supply that is used for processed liquid and circulation, circulating pump 31 and stopping alternately repeatedly, if it is big that the difference of come-up oil level 62 and processed liquid level 61 becomes, promptly accumulated oil slick on the top of separation portion 81, by in the running of supply pump 21, making 52 one-tenth closed conditions of valve of discharge pipe 51,12 one-tenth equal heights of processed liquid level 61 and shield, oil slick is overflowed from the upper end of shield 12, and upwards oil slick acceptance division 83 is discharged.
Because common screw compressor approximately accumulates oil slick 1mm by the continuous running in a week in oily-water seperating equipment 10, so go up the discharge of oil slick as long as carry out just passable with the frequency weekly.This efflux time also can determine by mensuration come-up oil mass, last oil slick thickness not only by the decision duration of runs.
This batch process in separation portion 81, is carried out water-oil separating with the processed liquid that is in the state of being untreated with roughly the same separately amount with the processed liquid after clear water or the processing and is handled, and oil content can drop to low concentration from high concentration at short notice.
Add calcium chloride or magnesium chloride and hydrochloric acid, sulfuric acid or nitric acid and NaOH and promote oil-water separation method as described later, if behind abundant mixed chlorinated calcium or magnesium chloride and processed liquid, add NaOH, it is big that oil-water separation becomes.
As previously mentioned, the amount of moisture in being equivalent to the atmosphere in summer for a long time, drain discharge is many, concentration of oil is low.Amount of moisture in being equivalent to the atmosphere in winter after a little while, drain discharge is few, the concentration of oil height.
Therefore, since many at drain discharge, when concentration of oil hangs down, outer (outside) cycle operation time of groove is short, and is few at drain discharge, when concentration of oil is high, outer (outside) cycle operation time of groove is long, but can constitute the oily-water seperating equipment 10 of the small-sized high speed processing of corresponding draining generating capacity.
Supply pump 21 in the running of above-mentioned oily-water seperating equipment 10, running and each valve 22 with circulating pump 31,36,39,42,52,77,97, the switch of 107 grades, the operator also can implement manual operation, be provided with the control device (control method) 200 that uses computer PC, described computer PC is equipped with and stores memory storage and being used to that control carries out the program of these operations and carry out the timer of its program and memory storage that record carries out state etc., in above-mentioned control device 200, store following performing a programme (second control method of carrying out first control method of first control and carrying out second control) in advance: the running that this program is carried out by this pump makes this external circulating system performance function (the 1st control); Supply with at least a, the calcium chloride water of hydrochloric acid, sulfuric acid and nitric acid or at least a and sodium hydrate aqueous solution of magnesium chloride brine by the 3rd～the 5th each pipe arrangement system; System sucks air, pressurizes in this pump by the 2nd pipe arrangement, and dissolved air in this processed liquid sprays (2nd control) as bubble with processed liquid from this nozzle, also can move automatically.
Outer (outside) cycle operation time of the groove in winter and summer can make and can select operation mode like that just as long as set by the timer of control device 200.
For the selection of these operation modes, the information of drain discharge or concentration of oil must be arranged.Owing to do not measure the method for concentration of oil at short notice, use the Information Selection operation mode of drain discharge.Drain discharge can be according to calculating such as the outlet temperature of the discharge air pressure of the amount of moisture in the atmosphere, air compressor, aerial cooler and condensed water arresting efficiencies.Thereby as long as measure atmospheric temperature and atmospheric humidity.
On the other hand, be typically provided with the case that accumulates from the draining of air compressor, also the liquid level meter can be installed therein, calculate drain discharge according to liquid level variation.In addition, only measure atmospheric temperature, the maximum stream flow of calculating atmospheric humidity and be 100% draining also can be used to control this value.In fact these gimmicks are used for alone or in combination control.The switching of these patterns also can be according to remaining on calendar on the not shown control device 200 etc., the switching that suits in advance.
As above illustrated, according to the present invention, even can high-speed separation place the also unseparated processed liquid of about profit half a year owing to contain the low oil of hydrophobicity.
Another embodiment of the present invention shown in Figure 2 is described.
Embodiment shown in Figure 1, the supply of hydrochloric acid, sodium hydrate aqueous solution and calcium chloride water is a driving force with the inlet pressure and the atmospheric pressure reduction of circulating pump 31, and the embodiment of Fig. 2 is to make sodium hydrate aqueous solution, calcium chloride water and the hydrochloric acid that the syringe 73,93 and 103 of dynamic formula is supplied with required amounts with resembling the air that moves back and forth the syringe, and attached have air pipe arrangement 74,94,104 and air to supply with control valve 75,95,105.
This embodiment can be not about operating condition institute for the external circulating system that comprises circulating pump 31 grades, in the separation portion 81 of treatment trough 11, supply with sodium hydrate aqueous solution, calcium chloride water and hydrochloric acid, can regulate quantity delivered arbitrarily with the amount of movement of syringe 73,93 and 103.
Another embodiment of the present invention shown in Figure 3 is described.
Embodiment shown in Figure 3 is provided with special-purpose weight feed pump 76,96 and 106 respectively in the pipe arrangement 72,92,102 from each case 71,91,101 of sodium hydrate aqueous solution, calcium chloride water and hydrochloric acid, about operating condition institute for the external circulating system that comprises circulating pump 31 grades, directly in the separation portion 81 of treatment trough 11, supply with sodium hydrate aqueous solution, calcium chloride water and hydrochloric acid from pipe arrangement 72,92,102, and can regulate its quantity delivered arbitrarily.
Another embodiment of the present invention shown in Figure 4 is described.
Embodiment shown in Figure 4 is provided with special-purpose weight feed pump 76,96 and 106 respectively in the pipe arrangement 72,92,102 from each case 71,91,101 of sodium hydrate aqueous solution, calcium chloride water and hydrochloric acid, the outlet (supply port) of pipe arrangement 72,92,102 is connected (continuously) with pipe arrangement 38, relief valve 39 in the running of circulating pump 31, supply with between flow periods in pipe arrangement 38 in processed liquid and add drug class.
About operating condition institute,, and can regulate its quantity delivered arbitrarily by direct supply sodium hydrate aqueous solution, calcium chloride water and the hydrochloric acid to the separation portion 81 of treatment trough 11 in of pipe arrangement 72,92,102 for the external circulating system that comprises circulating pump 31 grades.
The same with the embodiment of Fig. 1, owing to sodium hydrate aqueous solution, calcium chloride water supply to the processed liquid of the portion of separation 81 from pipe arrangement 38 with hydrochloric acid, fully mix with the processed liquid that separates portion 81.
Below, another embodiment of the present invention shown in Figure 5 is described.
This embodiment replaces the weight feed pump 76,96 and 106 of the embodiment of Fig. 3, special-purpose general supply pump 76,96 and 106 is set respectively, supply with sodium hydrate aqueous solution, calcium chloride water and hydrochloric acid by pipe arrangement 72,92,102 to annex solution upper tank 78a, 98a, 108a, the remaining liq after their annex solution of inside temporarily is full of case 78b, 98b, 108b is recovered to case 71,91,101 by pipe arrangement 80,100,110.
In this embodiment, sodium hydrate aqueous solution, calcium chloride water and hydrochloric acid pass through relief valve 77,97 and 107 from annex solution holding tank 78b, 98b, 108b, adjust the open hour of valve 77,97 and 107, can in separating the processed liquid of portion 81, quantitatively mix desired amount with 109 by pipe arrangement 79,99.
Secondly, another embodiment of the present invention shown in Figure 6 is described.
This embodiment is provided with the preliminary treatment case 24 that temporarily stores processed liquid that is connected with the supply port of the pipe arrangement 26 of supplying with processed liquid at the leading portion that the separation portion 81 to treatment trough 11 supplies with processed liquid, portion is provided with mixer 25 within it, is respectively equipped with special-purpose weight feed pump 76,96,106 in the pipe arrangement 72,92 and 102 from each case 71,91,101 of sodium hydrate aqueous solution, calcium chloride water and hydrochloric acid.
About operating condition institute for the external circulating system that comprises circulating pump 31 grades, in preliminary treatment case 24, supply with sodium hydrate aqueous solution, calcium chloride water and hydrochloric acid by pipe arrangement 72,92 and 102, processed liquid and interpolation drug class are mixed fully by running mixer 25.Can also regulate its quantity delivered arbitrarily.
With add that the well-mixed processed liquid of drug class finishes in the separating treatment running, shut off valve 42, circulating pump 31 stops back relief valve 22, by pipe arrangement 23, supplies with separation portions 81 by supply pump 21 from pipe arrangement 23,32,37.
In this embodiment, owing to can finish the mixing of processed liquid and interpolation drug class in the running of the water-oil separating in separation portion 81, single treatment the duration of runs can be very short.
Also can replace weight feed pump 76,96,106 in this embodiment, the medicine adding method of using Fig. 2, Fig. 5 is to preliminary treatment case 24 supply of chemical classes.In addition, pipe arrangement 23 also can be connected with pipe arrangement 37.
Secondly, another embodiment of the present invention shown in Figure 7 is described.
This embodiment is provided with sparge pipe 51 in the bottom of treatment trough 11, is provided with valve 52 therebetween.And leading portion from processed liquid to separation portion 81 that supply be provided with the preliminary treatment case 24 that temporarily stores processed liquid and within it portion be provided with mixer 25, in the pipe arrangement 72,92 and 102 of each case 71,91,101 of accommodating sodium hydrate aqueous solution, calcium chloride water and hydrochloric acid, be respectively equipped with the weight feed pump 76,96,106 of special use.
In the water-oil separating running, supply with processed liquid, limit running mixer 25 to preliminary treatment case 24, the limit supplies with, mixes sodium hydrate aqueous solution, calcium chloride water and hydrochloric acid from each case 71,91,101 by the weight feed pump 76,96,106 of special use respectively in turn in preliminary treatment case 24.
When the water-oil separating running finishes, at shut off valve 42, after circulating pump 31 is stopped, discharge the processed liquid of handling from the sparge pipe 51 that is located at separation portion 81 bottoms by relief valve 52, reach by 63 positions of representing (under the state of enforcement water-oil separating up to liquid level, become the processed liquid quantity delivered liquid level position during half amount approximately in separation portion 81), shut off valve 52.
Afterwards, make circulating pump 31 runnings, relief valve 22,42 is supplied with separation portion 81 and is added fully mixed processed liquid of drug class from pipe arrangement 23,32 by supply pump 21 by pipe arrangement 23.
This embodiment not only can be finished untreated processed liquid in the water-oil separating in separation portion 81 and add the mixing of drug class, and owing to having mixed the untreated processed liquid that adds drug class in the water-oil separating that can supply with in separation portion 81, single treatment the duration of runs can be shorter.
In addition, this embodiment also can replace weight feed pump 76,96,106, and the medicine adding method of using Fig. 2, Fig. 5 is to preliminary treatment case 24 supply of chemical classes.In addition, pipe arrangement 23 also can be connected with pipe arrangement 37.
Fig. 8 represents an example of the oil separation effect according to the present invention.
Even leave standstill more than six months from the draining of compressor, oil content also keeps the colloid shape as the anticorrosion lubrication prescription (trade name of Kobelcocompressor Co., Ltd.) of the particular oils of lubrication for screw-type compressor oil, the oil content separation of can not floating.This oil and pure water are mixed when causing the simulation draining, separate even leave standstill also come-up for a long time.
When the concentration of oil that makes this simulation draining makes the 300mg/L that equates with general helical compression machine drainge, every 1L draining is added more than the calcium chloride 1g, the treating apparatus of running Fig. 1, oily separation energy reaches draining benchmark 5mg/L.Even changing concentration of oil also is same result, with its characteristic of region representation that surrounds with OBC of Fig. 8.
As everyone knows, calcium chloride uses as food hardening agent, the effect that has charge neutrality and condense electronegative elaioleucite as the calcium of the metal ion of positive divalence.But calcium chloride uses as Snow Agent, when concentration is high, makes metal erosion.
Thereby when separating use calcium chloride, must reduce the addition of calcium chloride for oil.The moisture of compressor draining is that the moisture cohesion in the atmosphere forms, even lubricating oil pH value under admixture also is 4 to 6 acidity.Even add inorganic salts calcium chloride in this draining, the pH value is also constant, still is 4 to 6 acidity.
Also can carry out the method that oil separates even studied the various additions that reduce this calcium chloride, the result distinguishes if add in advance calcium chloride water, adding hydrochloric acid, to make the pH value be acidity below 5, then add sodium hydrate aqueous solution, make the pH value become alkalescence more than 7, it is easy that oil separates transfiguration, the pH value becomes 8 or more, the treating apparatus of running Fig. 1 if make, even the addition of calcium chloride be 50% when adding separately, oily separation also can reach below the draining benchmark 5mg/L.
When adding sodium hydrate aqueous solution, study the additive effect of the calcium chloride of the concentration of oil in the relative draining.Its characteristic of region representation that surrounds with the ODE of Fig. 8.
And then distinguish, if add calcium chloride in advance, adding hydrochloric acid, to make the pH value be acidity below 5, then add NaOH, make the pH value become alkalescence more than 7, it is easier that water-oil separating becomes, and the pH value becomes 8 or more, the treating apparatus of the Fig. 1 that turns round if make, even separating, 30% the when addition of calcium chloride is interpolation separately, oil also can arrive below the draining benchmark 5mg/L.
The region representation that surrounds with the ODE of Fig. 8 is studied the result of additive effect of the calcium chloride of the concentration of oil in the relative draining of this situation.As long as turn round in this zone, draining is exactly that alkalescent, metal material are difficult to oxidized corrosion.
If further reduce the addition of calcium chloride, even add NaOH, can not water-oil separating to draining benchmark 5mg/L.Its characteristic of region representation that surrounds with OAE of Fig. 5.Thereby line segment OC, OD, OE represent by further interpolation calcium chloride separately respectively and and use interpolation NaOH and add hydrochloric acid, the lower limit of the oil-water separation of the concentration of oil of relative draining.
Above-mentioned characteristic can be carried out following explanation.Promptly suppose calcium chloride (CaCl
2) addition is B1, if concentration of oil increases in the draining, concentration of oil is just can not separating oil arrive draining benchmark 5mg/L more than the A1.Therefore, add calcium chloride (CaCl as if component in order to B1
2) after, add NaOH (NaOH), make the method for draining alkalize, can separating oil arrive draining benchmark 5mg/L to concentration of oil A2.If concentration of oil is more than the A2, calcium chloride (CaCl
2) addition is that B1 can not water-oil separating.If the component in order to B1 adds calcium chloride (CaCl
2) after, add hydrochloric acid (HCl) and make draining become acid, add NaOH (NaOH) again, make the method for draining alkalize, be that A3 can separating oil arrive draining benchmark 5mg/L up to concentration of oil.If concentration of oil is more than the A3, calcium chloride (CaCl
2) addition is that B1 just can not water-oil separating.
As the another kind of material that promotes the oil cohesion magnesium chloride (MgCl that is considered to as the food hardening agent use is arranged
2), be used in combination with hydrochloric acid and NaOH as if the same with calcium chloride, can obtain the effect the same with Fig. 8.Calcium chloride and magnesium chloride also can and be used in the combination of hydrochloric acid and NaOH.
If as the another kind of material that promotes the oil cohesion, use the aluminium chloride of the compound of positive trivalent metal aluminium, than the flocculating result height of calcium chloride.But, can not use metal, the constituent apparatus difficulty because aluminum metal corrosivity is strong especially.And, the influence of worry to human body arranged, the confined trend of the use in water treatment.
Replace hydrochloric acid to use sulfuric acid, nitric acid that same effect is also arranged.
In addition, hydrochloric acid, sulfuric acid, nitric acid also can not use separately and and usefulness, wish hydrochloric acid and nitric acid and with making concentration decline, or make the blending ratio that does not become chloroazotic acid.
And then, calcium chloride (CaCl
2) and magnesium chloride (MgCl
2) also can and use.
More than the water-oil separating to mineral oil is illustrated in the explanation, but also can be used for the separation of edible oil.Because vegetable oil draining benchmark is 30mg/L, loose slightly, correspondingly the addition of calcium chloride, magnesium chloride, hydrochloric acid, NaOH etc. can tail off.
Claims (13)
1, a kind of oil-water separation method, this method is to supply with small bubble to the processed liquid of treatment trough, the oil content and the bubble that are included in the processed liquid are floated together, make the oil-water separation method of processed liquid water-oil separating, it is characterized in that, supply with bubble to processed liquid, described processed liquid has been supplied with at least a, calcium chloride in hydrochloric acid, sulfuric acid and the nitric acid and at least a and NaOH in the magnesium chloride.
2, oil-water separation method as claimed in claim 1 is characterized in that, after at least a at least a and calcium chloride and the magnesium chloride supplied with to processed liquid in hydrochloric acid, sulfuric acid and the nitric acid, supplies with NaOH.
3, oil-water separation method as claimed in claim 1 is characterized in that, either party at least a elder generation at least a and calcium chloride in hydrochloric acid, sulfuric acid and the nitric acid and the magnesium chloride supplies with to processed liquid.
4, oil-water separation method as claimed in claim 1 is characterized in that, after processed liquid is supplied with at least a in calcium chloride and the magnesium chloride, supplies with at least a in hydrochloric acid, sulfuric acid and the nitric acid.
5, oil-water separation method as claimed in claim 1, it is characterized in that, processed liquid contains the low oil content of hydrophobicity, by supplying with acid and flocculating agent to described processed liquid, make described processed liquid become acid state, supply with alkali after the cohesion of the oil content after water-oil separating taking place and separating, make described processed liquid become alkaline state, promote water-oil separating.
6, a kind of oily-water seperating equipment, this device is to supply with small bubble to the processed liquid of treatment trough, the oil content and the bubble that are included in the processed liquid are floated together, make the oily-water seperating equipment of processed liquid water-oil separating, it is characterized in that described device comprises: by pump from described treatment trough the processed liquid of sucking-off, pressurization, from the 1st pipe arrangement system that the external circulating system of the nozzle ejection that is located at described treatment trough bottom constitutes; Suction is located at the 2nd pipe arrangement system of air of the suction side of described pump; The 3rd at least a pipe arrangement of supplying with in hydrochloric acid, sulfuric acid and the nitric acid to the processed liquid of described treatment trough is; Supply with at least a the 4th pipe arrangement system in calcium chloride water and the magnesium chloride brine; With the 5th pipe arrangement system that supplies with sodium hydrate aqueous solution.
7, oily-water seperating equipment as claimed in claim 6 is characterized in that, described device also has the control device that carries out following operation, makes described pump running, and described external circulating system is played a role; Each pipe arrangement system by the described the 3rd～the 5th supplies with at least a, calcium chloride water in hydrochloric acid, sulfuric acid and nitric acid and at least a and sodium hydrate aqueous solution in the magnesium chloride brine; And suck air by described the 2nd pipe arrangement system, in described pump, pressurize, make air dissolves in described processed liquid, with bubble and processed liquid together by described nozzle ejection.
8, oily-water seperating equipment as claimed in claim 7 is characterized in that, described control device is made of the 1st control device and the 2nd control device: the 1st control device makes described pump running, and external circulating system is played a role; After the 2nd control device is supplied with at least a and sodium hydrate aqueous solution at least a, calcium chloride water in hydrochloric acid, sulfuric acid and nitric acid and the magnesium chloride brine by each pipe arrangement system of the described the 3rd～the 5th, by described the 2nd pipe arrangement is to suck air, in described pump, pressurize, make air dissolves in described processed liquid, spray by described nozzle together with bubble and processed liquid.
9, oily-water seperating equipment as claimed in claim 6, it is characterized in that, the suction side that this device has a described pump in described the 1st pipe arrangement system is provided with the supply port of pressure-regulating valve and described the 3rd pipe arrangement system to the 5th pipe arrangement system, by adjusting the aperture of described pressure-regulating valve, the pump intake pressure of described pump is forced down than atmosphere, supply with hydrochloric acid as driving force to described processed liquid with the pressure reduction of atmospheric pressure and described pump intake pressure, at least a in sulfuric acid and the nitric acid, at least a in calcium chloride water and the magnesium chloride brine, and the device of sodium hydrate aqueous solution.
10, as claim 6 to each described oily-water seperating equipment of claim 9, it is characterized in that, the exhaust end of the described pump from described the 1st pipe arrangement system, be provided with the bypass pipe arrangement system with switch valve from the pipe arrangement between described nozzle to described treatment trough, described switch valve becomes open state between described external circulating system performance functional period.
11, as the described oily-water seperating equipment of above-mentioned claim 8, it is characterized in that, behind at least a in supplied with at least a, calcium chloride water in hydrochloric acid, sulfuric acid and the nitric acid and magnesium chloride brine by described the 3rd, the 4th pipe arrangement system of described the 2nd control device, system supplies with sodium hydrate aqueous solution by the 5th pipe arrangement.
12, as above-mentioned claim 6 to each described oily-water seperating equipment of claim 9, it is characterized in that described device has each pipe arrangement system of the described the 3rd to the 5th supplies with at least a and sodium hydrate aqueous solution at least a, calcium chloride water in hydrochloric acid, sulfuric acid and the nitric acid of aequum and the magnesium chloride brine respectively to the processed liquid of described treatment trough device.
13, as above-mentioned claim 6 to each described oily-water seperating equipment of claim 9, it is characterized in that, be provided with the preliminary treatment case that the supply port with the supplying tubing of the 3rd to the 5th each pipe arrangement system and processed liquid is connected, in described treatment box, will supply with described treatment trough with at least a and mixed processed liquid of sodium hydrate aqueous solution at least a, calcium chloride water in hydrochloric acid, sulfuric acid and the nitric acid and the magnesium chloride brine.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2005227358 | 2005-08-05 | ||
| JP2005227358A JP2007038173A (en) | 2005-08-05 | 2005-08-05 | Oil and water separating method and oil and water separating apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1919403A true CN1919403A (en) | 2007-02-28 |
| CN100518877C CN100518877C (en) | 2009-07-29 |
Family
ID=37777327
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006101100572A Expired - Fee Related CN100518877C (en) | 2005-08-05 | 2006-08-04 | Method and apparatus for separating oil and water |
Country Status (3)
| Country | Link |
|---|---|
| JP (1) | JP2007038173A (en) |
| CN (1) | CN100518877C (en) |
| TW (1) | TW200709836A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102655920A (en) * | 2009-12-10 | 2012-09-05 | 株式会社Ihi | Oil-water separation device and refining device |
| CN105668954A (en) * | 2014-11-20 | 2016-06-15 | 中国石油化工股份有限公司 | Destabilizing reagent and a method therewith for treating polymer-bearing oil sludge in oil field |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5211636B2 (en) * | 2007-03-29 | 2013-06-12 | Ｊｆｅスチール株式会社 | Oil-containing wastewater treatment method and oil-containing wastewater treatment facility |
| CN112691512A (en) * | 2020-10-29 | 2021-04-23 | 茂裕环保科技南通有限公司 | But scrubbing tower with oil-water separation structure deodorization |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS53111649A (en) * | 1977-03-11 | 1978-09-29 | Nikko Eng | Method of treating waste water |
| JPH0235798B2 (en) * | 1981-01-22 | 1990-08-13 | Sankyo Juki Kk | HAIKIBUTSUKARANOABURANOKAISHUHOHO |
| JPS63133967A (en) * | 1986-11-26 | 1988-06-06 | Masashi Ishikawa | Production of fish meal having process for recovering protein of broth |
| JPH0632834B2 (en) * | 1987-12-29 | 1994-05-02 | 荏原インフイルコ株式会社 | Organic wastewater treatment method |
| CN1023072C (en) * | 1990-03-31 | 1993-12-15 | 沈汉石 | Method for separation of oil from water and oil purification equipment |
-
2005
- 2005-08-05 JP JP2005227358A patent/JP2007038173A/en active Pending
-
2006
- 2006-07-12 TW TW095125470A patent/TW200709836A/en not_active IP Right Cessation
- 2006-08-04 CN CNB2006101100572A patent/CN100518877C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102655920A (en) * | 2009-12-10 | 2012-09-05 | 株式会社Ihi | Oil-water separation device and refining device |
| US8864888B2 (en) | 2009-12-10 | 2014-10-21 | Ihi Corporation | Oil-water separation device and refining device |
| CN102655920B (en) * | 2009-12-10 | 2015-03-18 | 株式会社Ihi | Oil-water separation device and refining device |
| CN105668954A (en) * | 2014-11-20 | 2016-06-15 | 中国石油化工股份有限公司 | Destabilizing reagent and a method therewith for treating polymer-bearing oil sludge in oil field |
| CN105668954B (en) * | 2014-11-20 | 2018-12-28 | 中国石油化工股份有限公司 | A method of it breaking steady medicament and breaks steady chemicals treatment oil field polymer-containing oil sludge using this |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100518877C (en) | 2009-07-29 |
| TW200709836A (en) | 2007-03-16 |
| TWI294303B (en) | 2008-03-11 |
| JP2007038173A (en) | 2007-02-15 |
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